CN105026018A - Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both - Google Patents

Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both Download PDF

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Publication number
CN105026018A
CN105026018A CN201380074473.XA CN201380074473A CN105026018A CN 105026018 A CN105026018 A CN 105026018A CN 201380074473 A CN201380074473 A CN 201380074473A CN 105026018 A CN105026018 A CN 105026018A
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China
Prior art keywords
order
final stage
concentrate
intergrade
entrance
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CN201380074473.XA
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CN105026018B (en
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翟建文
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BL Technology, Inc.
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General Electric Co
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/145—Ultrafiltration
    • B01D61/146—Ultrafiltration comprising multiple ultrafiltration steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/58—Multistep processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/10—Spiral-wound membrane modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/08—Specific process operations in the concentrate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B01D2311/252—Recirculation of concentrate
    • B01D2311/2523—Recirculation of concentrate to feed side
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/24—Specific pressurizing or depressurizing means
    • B01D2313/243—Pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/02—Elements in series
    • B01D2317/022—Reject series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/145—Ultrafiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions

Abstract

A membrane filtration system with reverse osmosis (RO) or nanofiltration (NF) elements is adapted to provide high recovery from difficult wastewater. The system has a plurality of stages. The system is configured to provide concentrate staging. The last stage also has concentrate recirculation. The valves and pumps of the system are arranged such that the order of flow and a recirculation pump may be switched between the first stage and the last stage at some times.

Description

With concentrate classification and concentrate recirculation, convertible level or both membrane filtration systems
Technical field
This description relates to membrane filtration, such as counter-infiltration or nanofiltration.
Background technology
Counter-infiltration (RO) and nanofiltration (NF) film typically use with the form of element (also referred to as membrane module), such as spiral wound element, hollow fiber elements or tube element.Many elements typically between 1 to 8 are in series arranged in pressure vessel (being alternatively called housing), and it is with inlet, concentrated solution outlet and permeate outlet.Multiple pressure vessel can be connected in parallel on together with organizator in filtration system (being alternatively called level).The films that are jointly called at different levels of filtration system hinder.
Filtration system can have the multiple levels linked together with various structure.In concentrate classification (being alternatively called multiple stage array), supply water and be first pumped in the first order of element.Concentrate from each upstream stage is fed into each downstream stage.The concentrate interface of final stage is equipped with concentrate valve.The flowing hindered through film and pressure are by feed pump and concentrate Valve controlling.Penetrating fluid flows to public penetrating fluid main channel from each grade.Concentrate classification increases penetrating fluid and reclaims.Filtration system with the high-recovery of such as 80% or more typically has at least two levels.
Summary of the invention
Although concentrate classification increases the rate of recovery of system, the flow of concentrate declines in each level.For the waste water of some types, can be not enough to prevent the dirt in final stage from blocking up at the height flow reclaimed in filtration system.
In the filtration system that this description describes, two or more levels link together to provide concentrate classification.Final stage has the recirculation pump and conduit that are configured to provide concentrate to recycle.In another filtration system, the valve of arrangement system and conduit allow the to feed water order of the part and final stage that flow through the first order is converted.This part can be the whole first order or be less than the whole first order.Preferably, be with or without the order conversion of flowing, system in the end receives in the level of concentrate provides concentrate classification and concentrate recirculation.
In the filter process that this description describes, feedwater is divided into penetrating fluid and the first concentrate.First concentrate is divided into penetrating fluid and the second concentrate.A part for second concentrate part is recovered and mixes with the first concentrate.In another process, the order of flowing is changed sometimes between a part for the first order of filtration system and final stage.This part can be the whole first order, or is less than a part for the whole first order.Preferably, in each order, System Implementation has concentrate classification and the filter process both concentrate recirculation.
Accompanying drawing explanation
Fig. 1 is the schematic process flow diagram flow chart of filtration system.
Fig. 2 is the schematic process flow diagram flow chart of the second filtration system.
Fig. 3 is the schematic process flow diagram flow chart of the 3rd filtration system.
Detailed description of the invention
With reference to figure 1, filtration system 10 processes feedwater 12 to produce effluent 14.Filtration system has feed pump 22, the first order 16, final stage 20, recirculation pump 24 and salt solution 26.System 10 preferably also has one or more intergrade 18.In system 10, final stage 20 can be described as the third level, but final stage 20 can be the second level, the fourth stage or another level in other systems.And in system 10, but intergrade 18 can be described as intergrade in other system of the second level can comprise the level of the second level, the third level, the fourth stage or more.
Each grade comprises the group of one or more film filtering element, and film filtering element is such as nanofiltration or ro components.Multiple elements in level typically in series provide in pressure vessel.Larger level can comprise in parallel with multiple pressure vessels that water pipe connects, such as with the entrance of each be connected in 8 pressure vessels feed liquor manifold, be connected to the concentrate manifold of the concentrated solution outlet of each in 8 pressure vessels and be connected to the permeate manifold of the permeate outlet of each in 8 pressure vessels.Intergrade 18 that the first order 16 is preferably more than (that is, having the element of more formed objects).Final stage 20 is preferably more than intergrade 18.The first order 16 is preferably at least equally large with final stage 20.
Filtration system also has valve V1 to V9 and is configured to provide the various pipelines of flow path described below.Valve V1 to V9 can move between fully open and fully closed position.But valve V9 preferably can be set to the choke valve in various centre position.The flowing hindered through film and pressure are controlled by both feed pump 22 or valve V9 or they.
In the shown first structure, valve V1, V3, V5 and V7 open.Valve V2, V4, V6 and V8 close.Valve V9 opens the salt solution providing outflow with the flow selected at least in part.System 10 also can closing with valve V1, V3, V5 and V7, valve V2, V4, V6 and V8 open and running in valve V9 opens at least in part the second structure.In two kinds of structures, the flow of salt solution 26 is preferably 20% or less of the flow of feedwater 22.80% or more of feedwater 22 is recovered as penetrating fluid 14.
In the first structure, feedwater 12 is pumped to the first order 16 by feed pump 22.First order penetrating fluid 28 produces and becomes a part for effluent 14.First order concentrate 30 also produces and flows to intergrade 18.The first order concentrate 30 flowing through the liquid feeding side of intergrade 18 is divided into second level penetrating fluid 32 and second level concentrate 34.Second level penetrating fluid 32 becomes a part for effluent 14.Second level concentrate 34 flows to recirculation pump 24.Second level concentrate 34 is pumped to final stage 20 by recirculation pump 24.Third level penetrating fluid 36 produces and becomes a part for effluent 14.Third level concentrate 38 is partly discharged as salt solution 26, and is partly back to the liquid feeding side of recirculation pump 24.A part for third level concentrate 38 is recycled to the third level 20 thus.In a word, system 10 operates with concentrate classification between level 16,18,20 and recycles with concentrate in final stage 20.
In the second configuration, system 10 operates with concentrate classification between level 16,18,20 and again with concentrate recirculation in the level in the end receiving concentrate.But first the third level 20 receives feedwater 12 in this case; The direction of concentrate classification is from the third level 20 to the second level 18 to the first order 16; And the first order 16 operates with concentrate recovery, is alternatively called feed liquor and outflow.
The order of recirculation pump 24 and flowing is being changed through the first order 16 and final stage 20 when valve moves to the second structure from the first structure.But preferably, the direction through the flowing of the liquid feeding side of level 16,18,20 is not changing when valve moves to the second structure from the first structure.Although some elements and pressure vessel can be configured to reversible flowing, other have only operate with along a direction flowing or optimize for the such as brine seal part of the flowing along a direction or the component of permeate collection device.In the system with multiple intergrade, the order of the flowing between intergrade is not also preferably changing when valve moves to the second structure from the first structure.The relative number of element or pipeline or pumping system also can optimize between multiple centre along the flowing in a direction.
The use of concentrate classification allows high-recovery, and such as 80% or more or between 85% to 95%.The flow that concentrate recirculation in final stage increases through final stage blocks up to contribute to suppressing dirty.Because first and second grades in rational liquid feeding side concentrate running, overall penetration liquid quality keeps higher.Cost and the energy ezpenditure of recirculation pump are limited to required for final stage.But in some cases, final stage can be still dirty stifled.When having at least, the order of switching flows allows final stage to be rinsed to contribute to further suppression with feedwater or remove dirty stifled in some cases.Especially, although there is concentrate to recycle, some the solvable organic compounds in very unmanageable waste water can cause the dirt in final stage to be blocked up.But, sometimes make final stage be exposed to unconcentrated feedwater and dirty for organic matter blocking layer is rinsed from final stage.In system 10, final stage 20 can be changed with the first order 16 and receive the half of unconcentrated feedwater 12 up to the duration of runs of system 10.
For the ease of conversion, the first order 16 and the second level 20 are preferably formed objects, or at least approximately identical size.If the first order 16 is greater than final stage 20 significantly, so final stage can be changed with a part for the first order 16 being less than the whole first order 16.In this case, this part is preferably and final stage 20 formed objects, or at least approximately identical size.Such as, the part of the first order 16 changed with final stage 20 (can be the whole first order 16 or be less than the whole first order) can have many elements or pressure vessel or both, its in final stage 20 corresponding number or multiple number 25% in.
System 10 can be used to process diversified feedwater 12.But system 10 is suitable for providing the height (80% or more) from very unmanageable waste water to reclaim especially.Feedwater 12 can have the COD (COD) of 200mg/L or more.Unmanageable waste water comprises such as percolate, coking plant wastewater, counter-infiltration salt solution and cooling tower sewer.Alternatively, recovery can increase further by process salt solution, such as, use hot vaporizer, crystallizer, zero liquid drains (ZLD) or thing amount-chemical processing system.
example
In a first example, three grades of nanofiltration (NF) systems 10 are designed for the COD (COD), the 90m that are greater than 200mg/L 3the permeate flow of/h and 90% is retrieved to process trade effluent.System 10 is arranged as shown in FIG. 1.Feed pump 22 is rated for 100m 3the output of/h and the high-pressure pump of 110m head.Recirculation pump 24 is rated for 110m 3the output of/h and 40m head.
System has 126 nominals, 8 inches of (20cm) NF spiral wound element, and it inserts 21 pressure vessels.Each pressure vessel in series keeps 6 elements.System has three levels 16,18,20.The first order 16 and final stage 20 have separately in parallel with 8 pressure vessels that water pipe is connected.Intergrade has in parallel with 5 pressure vessels that water pipe connects.
First and final stage 16,18 be same, and the order of recirculation pump 24 and flowing can be changed between which.In a valve constitution, as shown in FIG. 1, valve V1, V3, V5 and V7 open, and valve V2, V4, V6 and V8 close.Feedwater 12 is pumped into the first order 16 by high pressure feed pump 22, and the concentrate from the first order 16 is supplied to intergrade 18, and is supplied to final stage 20 from the concentrate of intergrade 18 through recirculation pump 24.In the second valve constitution, wherein the first order 16 and final stage 20 are changed, and valve V2, V4, V6 and V8 open, and valve V1, V3, V5 and V7 close.Feedwater 12 is pumped into final stage 20 by high-pressure pump, and the concentrate from the third level 20 is supplied to intergrade 18, and is supplied to the first order 16 from the concentrate of intergrade 18 through recirculation pump 24.In two kinds of structures, valve V9 is the control valve that running controls concentrate flowing.The 6-8m of every NF element is realized in all levels 3the concentrate of the high cross flow of/h.
In the second example, show in fig. 2, second system 40 is designed for COD, 90m more than 200mg/L 3the permeate flow of/h and 95% is retrieved to process trade effluent.Second system 40 has four levels 16,18,19 and 20.The first order is divided into two parts, Part I 16A and Part II 16B.The order of recirculation pump 24 and flowing can be changed between final stage 20 and the Part I 16A of the first order 16.When changing, the Part I 16A of the first order 16 finally receives concentrate, and first final stage 20 receives feedwater in parallel with the Part II 16B of the first order.
Feed pump 22 is rated for 100m 3the output of/h and the high-pressure pump of 110m head.Second system also has and is rated for 40m 3the booster pump 46 of the output of/h and 30m head and be rated for 56m 3the output of/h and the recirculation pump 24 of 40m head.
NF system has 138 nominals, 8 inches of (20cm) NF elements, and it inserts 23 pressure vessels.Each pressure vessel in series keeps 6 elements.The first order 16 has eight pressure vessels.In these pressure vessels, five connect with water pipe in parallel and form Part I 16A.Remaining three pressure vessels connect with water pipe in parallel and form Part II 16B.First intergrade 18 has in parallel with six pressure vessels that water pipe connects.Second intergrade 19 has in parallel with three pressure vessels that water pipe connects.Final stage 20 has in parallel with five pressure vessels that water pipe connects.Part I 16A and the third level 20 are same as to contribute to conversion between which.Part II 16B receives all the time directly from the feedwater 12 of feed pump 22.
When valve constitution becomes in as Fig. 2 the first structure shown, valve V1, V3, V5 and V7 open, and valve V2, V4, V6 and V8 close.Feedwater 12 is pumped into Part I 16A and the Part II 16B of the first order 16 by feed pump 12.Concentrate from the first order 16 is supplied to the first intergrade 18, is then supplied to the second intergrade through booster pump 46.Concentrate from the second intergrade 19 is supplied to final stage 20 through recirculation pump 24.Make Part I 16A and final stage 20 change when valve constitution becomes the second structure, valve V2, V4, V6 and V8 open, and valve V1, V3, V5 and V7 close.Feedwater 12 is pumped into final stage 20 and Part II 16B by high-pressure pump 22.Concentrate from final stage 20 and Part I 16B is supplied to the first intergrade 18, is then supplied to the second intergrade through booster pump 46.Concentrate from the second intergrade 19 is supplied to Part I 16A through recirculation pump 24.Valve V9 is used as control valve to control the concentrate flowing in two kinds of structures.
Alternatively, although do not show in fig. 2, the valve of second system 40 and conduit can change, and make another part selected of the first order 16 sometimes finally receive concentrate, and first final stage 20 and the remaining first order receive feedwater in parallel.But, expect that the part of the first order 16 changed with final stage 20 has element and the pressure vessel of the identical number with final stage 20, recirculation pump 24 and second system 40 are integrally worked in two structures good.In second system 20, as the result of optimization system design, the first order 16 does not have the pressure vessel of the twice of the pressure vessel of final stage 20.Although five in eight of the first order 16 pressure vessels what change with final stage 20 will be alternately possible, but because the main purpose of the order of switching flows allows final stage 20 to have the period being exposed to unconcentrated feedwater 12, so this complexity is typically irrational.If the first order 16 has element and the pressure vessel 20 of twice by chance, what part and the final stage 20 of the first order 16 were changed alternately will be easier.But in most cases, ability final stage 20 and any portion 16A, the 16B in the first order 16 changed will verify the optimal selection of the number changing element in each grade and pressure vessel.Dirt in these suggestions hypothesis final stage 20 is blocked up and is reached the half of system duration of runs by final stage 20 being exposed to unconcentrated feedwater 12 or less coming to control fully.If can not, the half that so system can be modified to allow the method operated to make the pressure vessel of the first order 16 exceed the duration of runs finally receives concentrate, but the pressure vessel that the system replaced between them causes each independent finally receives the half that concentrate is less than the duration of runs.
In the 3rd example, show in figure 3, the 3rd system 42 is designed for COD, 90m more than 200mg/L 3the permeate flow of/h and 90% is retrieved to process trade effluent.Recirculation pump 24 is for final stage 20.3rd system 42 is similar to the system 10 of Fig. 1, but the valve not allowing the order of the first order 16 and final stage 20 to be inverted and conduit.
3rd system 42 has 126 nominals, 8 inches of (20cm) NF elements, and it inserts 21 pressure vessels.Each pressure vessel in series keeps 6 elements.High pressure feed pump 22 is rated for 100m 3the output of/h and 110m head.Recirculation pump 24 is rated for 110m 3the output of/h and 40m head.3rd system 42 has three levels 16,18,20.The first order 16 and final stage 20 have separately in parallel with 8 pressure vessels that water pipe is connected.Intergrade 18 has in parallel with 5 pressure vessels that water pipe connects.Feedwater 12 is pumped into the liquid inlet of the first order 16 by high pressure feed pump 22.Concentrate from the first order 16 is supplied to the liquid inlet of intergrade 18.Concentrate from intergrade 18 passes the liquid inlet that recirculation pump 24 is supplied to the third level 20.
This written description uses example with open the present invention and enables any technical staff of this area put into practice the present invention, comprises and manufactures and use any device or system and perform the method be incorporated to arbitrarily.Of the present inventionly patented scope can be defined by the claims, and other examples that those skilled in the art expect can be comprised.

Claims (19)

1. a membrane filtration system, comprising:
A) first order;
B) final stage;
C) feed pump;
D) recirculation pump;
E) brine outlet; And,
F) conduit group, it is suitable for connecting: the outlet side of described feed pump is to the entrance of the described first order; The concentrated solution outlet of the described first order is to the entrance of described recirculation pump; And the entrance being exported to described final stage of described recirculation pump; The concentrated solution outlet of described final stage is to described brine outlet and to the described entrance of described recirculation pump.
2. system according to claim 1, is characterized in that, also comprises the first intergrade, and the described concentrated solution outlet of the described first order is connected to the described entrance of described final stage by wherein said conduit group through the liquid feeding side of described first intergrade.
3. system according to claim 2, is characterized in that, also comprises the second intergrade, and the concentrated solution outlet of described first intergrade is connected to the described entrance of described final stage by wherein said conduit group through the liquid feeding side of described second intergrade.
4. system according to claim 3, is characterized in that, is also included in the concentrate booster pump between described first intergrade and described second intergrade.
5. the system according to any one in claim 2 to 4, is characterized in that, the described first order is greater than described first intergrade, and described final stage is greater than described first intergrade.
6. the system according to any one in claim 1 to 5, is characterized in that, also comprises valve group, and wherein said valve group and described conduit group are suitable for the order of optionally switching flows between the part and described final stage of the described first order.
7. system according to claim 6, is characterized in that, the described part of the first order has the filter element of identical number in the pressure vessel of the parallel connection of identical number.
8. the system according to any one in claim 6 or 7, it is characterized in that, a () described first order is formed objects about with described final stage, and the described part of the described first order is the whole first order, or (b) the described first order is greater than described final stage, and the described part of the described first order is less than the described whole first order but formed objects about with described final stage.
9. the system according to any one in claim 1 to 8, is characterized in that, described valve group and described conduit group are suitable for optionally the outlet side of described feed pump being connected to the described entrance of described final stage or described concentrated solution outlet.
10. the system according to any one in claim 1 to 9, is characterized in that, described valve group and described conduit group are suitable for optionally the described outlet of described recirculation pump being connected to the described entrance of a part for the described first order or described concentrated solution outlet.
11. systems according to any one in claim 1 to 10, it is characterized in that, described valve group is suitable for optionally being connected with described conduit group: the described outlet side of described feed pump is to the described entrance of described final stage; The described concentrated solution outlet of described final stage is to the described entrance of described recirculation pump; The described entrance of a part for the described first order or the described first order is exported to described in described recirculation pump; The described concentrated solution outlet of the described part of the described first order or the described first order is to described brine outlet and to the described entrance of described recirculation pump.
12. 1 kinds of membrane filtration systems, comprising:
A) first order;
B) final stage;
C) feed pump;
D) brine outlet; And,
E) group of conduit and valve, it to be suitable for providing from described feed pump through the described first order and described final stage to the flowing of described brine outlet, and is suitable for the order of the flowing between the part and described final stage of the described first order is optionally changed,
Wherein, nonreversible through the direction of the flowing of level when the order conversion of described flowing.
13. systems according to claim 12, is characterized in that, also comprise recirculation pump, and the group of wherein said conduit and valve is suitable for enabling described recirculation pump optionally be connected to the described part of the described first order or described final stage.
14. 1 kinds of processes processing feedwater, comprise the step of multiple grades making described feedwater flow through the membrane filtration with the concentrate classification between described level and the recirculation of the concentrate in described final stage.
15. processes according to claim 14, it is characterized in that, also comprise and make described feedwater periodically flow through the step of described multiple grades recycling the membrane filtration changed between the part and described final stage of the described first order with the order flowed and concentrate.
16. 1 kinds of processes processing feedwater, comprise the step making described feedwater flow through multiple grades of membrane filtration, the order wherein flowed is changed sometimes between a part for the first order and final stage, and the nonreversible direction flowing through the described part of the described first order or the liquid feeding side of described final stage.
17. according to claim 14 to the process described in any one in 16, and it is characterized in that, described level comprises the spiral membrane module of nominal 8 inches, and is at least 6m through the described feed liquor of each grade or concentrated solution discharge 3/ h.
18., according to claim 14 to the process described in any one in 17, is characterized in that, described process with 80% or more rate of recovery running.
19. according to claim 14 to the process described in any one in 18, and it is characterized in that, described feedwater has the COD of at least 200mg/L.
CN201380074473.XA 2013-03-14 2013-03-14 Membrane filtration system with concentrate classification and concentrate recycling, convertible grade or both Active CN105026018B (en)

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Application Number Priority Date Filing Date Title
PCT/CN2013/072588 WO2014139116A1 (en) 2013-03-14 2013-03-14 Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both

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CN105026018A true CN105026018A (en) 2015-11-04
CN105026018B CN105026018B (en) 2019-10-29

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CN110180393A (en) * 2019-05-31 2019-08-30 浙江理工大学 Reverse osmosis advanced enrichment facility and method
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CN115520934B (en) * 2021-06-25 2024-05-03 中国石油化工股份有限公司 Membrane separation recovery system and method

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